CN105627694A - System and method for compression, liquefaction and recovery of BOG in LNG filling station - Google Patents
System and method for compression, liquefaction and recovery of BOG in LNG filling station Download PDFInfo
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- CN105627694A CN105627694A CN201610143911.9A CN201610143911A CN105627694A CN 105627694 A CN105627694 A CN 105627694A CN 201610143911 A CN201610143911 A CN 201610143911A CN 105627694 A CN105627694 A CN 105627694A
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- 238000011084 recovery Methods 0.000 title claims abstract description 47
- 230000006835 compression Effects 0.000 title claims abstract description 44
- 238000007906 compression Methods 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000009413 insulation Methods 0.000 claims abstract description 67
- 239000007789 gas Substances 0.000 claims description 77
- 239000007788 liquid Substances 0.000 claims description 32
- 238000003860 storage Methods 0.000 claims description 30
- 239000012071 phase Substances 0.000 claims description 12
- 239000007792 gaseous phase Substances 0.000 claims description 5
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- 239000007791 liquid phase Substances 0.000 claims description 3
- 239000000203 mixture Substances 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 3
- 235000019628 coolness Nutrition 0.000 claims description 2
- 239000012530 fluid Substances 0.000 claims description 2
- 238000007710 freezing Methods 0.000 claims description 2
- 230000008014 freezing Effects 0.000 claims description 2
- 238000002309 gasification Methods 0.000 abstract description 2
- 239000003949 liquefied natural gas Substances 0.000 abstract 4
- 238000005457 optimization Methods 0.000 abstract 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000003912 environmental pollution Methods 0.000 description 3
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 238000005057 refrigeration Methods 0.000 description 2
- 235000001674 Agaricus brunnescens Nutrition 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
- F25J1/0025—Boil-off gases "BOG" from storages
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
- F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C13/00—Details of vessels or of the filling or discharging of vessels
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0035—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by gas expansion with extraction of work
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
- F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
Landscapes
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
The invention relates to the technical field of overall station recovery for BOG generated by liquefied natural gas in LNG filling stations due to heat-loss gasification, specifically relates to a system and a method for compression, liquefaction and recovery of BOG in an LNG filling station, and particularly relates to an optimization design in a re-liquefaction system. According to the invention, a first-stage compressor and a vacuum heat-insulation three-in-one heat exchanger are driven by a heat-insulation expander; and the system and the method have the characteristics of being investment-saving, low in running expense, short in process flow, convenient for equipment skidding, and the like, and is quite suitable for being popularized in the LNG filling station.
Description
Technical field
The present invention relates in LNG gas station the BOG recovery technology field produced, be specifically related to a kind of to adopt expanding compress all-in-one, the LNG gas station BOG of vacuum insulation three-in-one spiral traverse baffle shell and tube heat exchanger compresses and liquefies recovery system, and adopts the method for described system recoveries BOG.
Background technology
Along with the arrival of " rare-view set-up ", global energy center of gravity to more efficiently, the natural gas energy resource fast transfer of environmental protection more. LNG automobile, as country's clean energy car, obtains the development advanced by leaps and bounds in recent years, simultaneously also carrying out the like the mushrooms after rain construction of big area of LNG gas station. At present in LNG gas station operational process, because of reasons such as condition of storage are harsh, design technology is not advanced, nearly all gas station all faces comparatively serious energy dissipation, and wherein the most outstanding is that BOG is recycled problem.
In LNG gas station production and operation process, due to the transport of LNG tank car, storage tank evaporate, unload, pressure regulation, precooling, pipeline heat absorption, storage tank flash distillation and pump work outward the reason such as defeated all can produce a large amount of BOG gas. BOG gas not only causes station system pressure to raise, and more brings bigger potential safety hazard, and finally this part BOG gas has to carry out diffusing safely, causes huge energy dissipation and financial loss.
Summary of the invention
This patent aims to provide a kind of BOG adopting expanding compress all-in-one, vacuum insulation three-in-one spiral traverse baffle shell and tube heat exchanger in LNG gas station and optimizes and compress and liquefy retrieving arrangement, solve the potential safety hazard of current LNG gas station and BOG gas emptying process cause environmental pollution, the wasting of resources.
For realizing above-mentioned technical purpose, the present invention adopts following technical scheme:
LNG gas station BOG compresses and liquefies recovery system, comprises the LNG storage tank for storing LNG liquid and the BOG surge tank for collecting BOG gas in gas station pipeline; LNG storage tank is connected by the one-level heat transfer zone of pipeline with vacuum insulation trinity interchanger respectively with described BOG surge tank; The compressor that all-in-one is compressed with adiabatic expansion in the one-level heat transfer zone of described vacuum insulation trinity interchanger is connected, the compressor of described adiabatic expansion compression all-in-one is connected with two stage compressor by one-level air temperature type interchanger, and described two stage compressor is connected by the one-level heat transfer zone of two grades of air temperature type interchanger with vacuum insulation trinity interchanger; The adiabatic expansion machine that all-in-one is compressed with adiabatic expansion in three grades of heat transfer zone of described vacuum insulation trinity interchanger is connected; The adiabatic expansion machine of described adiabatic expansion compression all-in-one connects gas-liquid separator, the gas phase mouth of described gas-liquid separator is connected with two grades of heat transfer zone of variable valve with described vacuum insulation trinity interchanger by pipeline, the liquid phase mouth of described gas-liquid separator connects cryopump, and described cryopump is connected with three grades of heat transfer zone and the described LNG storage tank of described vacuum insulation trinity interchanger.
As preferably, three tubular heat exchangers are integrated in a vacuum shell by described vacuum insulation trinity interchanger, adopting helical baffles to improve heat exchange efficiency in shell, part pipeline is integrated in shell, makes device miniaturization, and investment economizes, and joins pipe simple, and technique simplifies. Certainly, it is also possible to adopting other forms of three interchanger to be integrated in a vacuum shell, part pipeline is integrated in shell.
As preferably, described expanding compress all-in-one drives compressor while utilizing adiabatic expansion machine to carry out freezing, the BOG after rich heat being carried out one stage of compression, refrigerating efficiency height, equipment is little, and investment economizes, and technique simplifies, energy-saving and cost-reducing.
As preferably, described BOG compresses and liquefies recovery system and adopts DCS to be reclaimed by BOG to compress and liquefy sled and control, mutually chain, safe and reliable, simple to operate with pressure unit, temperature transmitter and fluid level transmitter respectively by variable valve.
As preferably, the gas phase portion of LNG tank car is connected by the pipeline of pipeline with described BOG surge tank top, and pipeline arranges vacuum breaker respectively. Described BOG compresses and liquefies recovery system and is not only reclaimed by the BOG in LNG storage tank, and all can be reclaimed by the BOG gas in LNG tank car and pipeline, has stopped the energy dissipation in gas station.
As preferably, described stage compressor and two stage compressor adopt one-level air temperature type interchanger and two grades of air temperature type interchanger to carry out inter-stage condensation, thus provide cold energy needed for BOG liquefaction of gases.
As preferably, described vacuum insulation trinity interchanger comprises shell and interior courage, vacuum vacuum shell is formed between described shell and interior courage, some heat transfer tubes of described vacuum insulation trinity interchanger are integrated to be arranged at described interior courage inside and forms described one-level heat transfer zone, two grades of heat transfer zone and three grades of heat transfer zone, and each heat transfer zone tubular heat exchanger adopts helical baffles to improve heat transfer efficiency.
As further preferably, the pipe journey between the one-level heat transfer zone of described vacuum insulation trinity interchanger and two grades of heat transfer zone, between two grades of heat transfer zone and three grades of heat transfer zone is connected by pipe journey connection chamber respectively; Shell side between the one-level heat transfer zone of described vacuum insulation trinity interchanger and two grades of heat transfer zone, between two grades of heat transfer zone and three grades of heat transfer zone is connected by shell side pipe connecting respectively.
Another object of the present invention is to provide the method adopting the above system recoveries BOG, comprise the steps:
S1. being collected in surge tank by the pipeline BOG of LNG gas station, and install variable valve at the gaseous phase outlet of surge tank, the gas phase of unloading unit also connects pressure recovery sled by this variable valve; The gaseous phase outlet of LNG storage tank is installed variable valve and is connected with pressure recovery sled; The pressure treated in storage tank exceedes the requirement of regulation, and chain promoter pressure recovery is prized by DCS, is reclaimed by BOG gas in LNG storage tank, and after LNG storage tank pressure is reduced to the value of regulation, DCS will stop pressure recovery; When BOG surge tank pressure reaches certain value, chain promoter pressure recovery is prized by DCS, and after pressure is reduced to the pressure of regulation, pressure recovery device will stop automatically; After LNG tank car has been unloaded, reclaim sled by BOG and NG in tank car is fully reclaimed. The BOG gas reclaimed carries out one-level heat exchange by sending into the vacuum insulation trinity interchanger of recovery device of liquefied after pressure regulation respectively, fully reclaims the cold energy of BOG gas;
S2. in vacuum insulation trinity interchanger, the compression NG of low temperature BOG gas and normal temperature carries out one-level heat exchange, makes BOG gas temperature rise to about 20 DEG C, becomes NG, by its cold energy all by compressing rear NG gas recovery;
S3., then NG sends into first step compressor boost, and stage compressor utilizes the mechanical energy of adiabatic expansion refrigerator to drive, and adiabatic expansion machine and stage compressor are incorporated on a support, not only invest province, save floor space, and refrigerating efficiency improves 70%, economize on electricity 40%. NG after compression sends into high stage compressor, is compressed to 10MPa, and two stages of compression adopts inter-stage condensation, makes the NG gas temperature after compression control at about 30 DEG C, then compression NG delivers to vacuum insulation trinity interchanger and lowers the temperature;
S4. compress NG in vacuum insulation trinity interchanger, to reclaim after BOG, gas-liquid separator part LNG in NG and gas-liquid separator respectively with low temperature carry out three grades of heat exchange, make compression NG gas temperature be down to about-110 DEG C; Then NG is sent into adiabatic expansion machine, makes NG pressure be down to 400KPa, owing to NG thermal insulation acting temperature is down to about-160 DEG C; Major part NG is liquefied.
S5. gas-liquid mixture is sent into gas-liquid separator, it is achieved gas-liquid separation; Gaseous state low temperature NG is by delivering to the two grades of heat exchange of vacuum insulation trinity interchanger after variable valve pressure regulation, a LNG part is pumped to LNG storage tank, and another part delivers to the vacuum insulation trinity interchanger third stage and compression NG heat exchange; In three grades of interchanger, LNG temperature rises to-120 DEG C and is gasificated into low temperature NG, the low temperature NG going out three grades of interchanger enters the two grades of heat exchange of vacuum insulation trinity interchanger by shell side pipe connecting in integrated heat exchanger together with gas-liquid separator low temperature NG, and heat exchange enters first-class heat exchanger and cooled by compression NG gas together with reclaiming BOG after terminating; Enter secondary heat exchanger from inter-stage pipe journey chamber respectively after compression NG is cooled from first-class heat exchanger, after two grades of coolings, enter again three grades of interchanger enter cooling; In vacuum insulation trinity interchanger, traverse baffle is spiral plate, it is to increase heat exchange efficiency 30%.
The present invention has at least following useful effect: the mechanical energy produced when adopting low temperature BOG adiabatic expansion to freeze drives compressor, the BOG after rich heat is carried out one stage of compression simultaneously, reduces energy consumption, it is to increase refrigerating efficiency; Adopt vacuum insulation trinity interchanger to realize the liquefy cold energy of each workshop section of BOG compression refrigeration to make full use of, enhance heat transfer efficiency, it is to increase the liquefaction efficiency that BOG reclaims; Adopt DCS that BOG recovery is compressed and liquefied sled to control, safe and reliable, simple to operate, it is beneficial to the potential safety hazard reducing LNG gas station, and BOG gas high efficiente callback can be realized, thus avoid BOG gas emptying to process the environmental pollution and the wasting of resources caused.
Accompanying drawing explanation
The following drawings is only intended to the present invention be done schematic description and interpretation, not delimit the scope of the invention. Wherein:
Fig. 1 is the structural representation of embodiment of the present invention recovery system;
Fig. 2 is the structural representation of three grades of tubular heat exchangers;
Fig. 3 is the structure for amplifying schematic diagram at A place in Fig. 2;
Fig. 4 is the structure for amplifying schematic diagram at B place in Fig. 2.
In figure: 1-LNG storage tank; 11,21,81-pipeline; 12,22,82-variable valve; 13,23,83-pressure unit; 2-BOG surge tank; 3-vacuum insulation trinity interchanger; 31-one-level heat transfer zone; 32-bis-grades of heat transfer zone; 33-tri-grades of heat transfer zone; 34-shell; Courage in 35-; 351-helical baffles; 36-vacuum shell; 37-heat transfer tube; 38-shell side; 381-shell side pipe connecting; 39-pipe journey; 391-pipe journey connection chamber; 4-adiabatic expansion compression all-in-one; 41-compressor; 42-adiabatic expansion machine; 5-one-level air temperature type interchanger; 6-bis-grades of air temperature type interchanger; 7-two stage compressor; 8-gas-liquid separator; 9-cryopump; 10-LNG tank car; 101-pipeline; 24,102-vacuum breaker.
Embodiment
Below in conjunction with drawings and Examples, set forth the present invention further. In the following detailed description, some one exemplary embodiment of the present invention is only described by the mode of explanation. Undoubtedly, it will also be recognized by those skilled in the art that, when without departing from the spirit and scope of the present invention, it is possible to by various different mode, described embodiment is revised. Therefore, accompanying drawing and description are being explanation property in essence, instead of for limiting the protection domain of claim.
As shown in Figures 1 to 4, LNG gas station BOG compresses and liquefies recovery system, comprises the LNG storage tank 1 for storing LNG liquid and the BOG surge tank 2 for collecting BOG gas in gas station pipeline, described LNG storage tank 1 is connected by the shell side 38 of pipeline 11,21 with the one-level heat transfer zone 31 of vacuum insulation trinity interchanger 3 respectively with described BOG surge tank 2 gas phase portion, the compressor 41 that the shell side 38 of the one-level heat transfer zone 31 of described vacuum insulation trinity interchanger 3 compresses all-in-one 4 with described adiabatic expansion is connected, the compressor 41 of described adiabatic expansion compression all-in-one 4 is connected by the pipe journey 39 of air temperature type interchanger 5 with the one-level heat transfer zone 31 of described three grades of tubular type vacuum insulation trinity interchanger 3, and described two stage compressor 7 is connected by the one-level heat transfer zone 31 of two grades of air temperature type interchanger 6 with vacuum insulation trinity interchanger 3, the adiabatic expansion machine 42 of the Guan Chengyu expanding compress all-in-one 4 of three grades of heat transfer zone 33 of described vacuum insulation trinity interchanger 3 is connected, the adiabatic expansion machine 42 of described adiabatic expansion compression all-in-one 4 connects gas-liquid separator 8, the gas phase mouth of described gas-liquid separator 8 is connected by the shell side 38 of pipeline 81 with two grades of heat transfer zone 32 of described vacuum insulation trinity interchanger 3, the liquid phase mouth of described gas-liquid separator 8 connects cryopump 9, described cryopump 9 is connected with three grades of heat transfer zone 33 and the described LNG storage tank 1 of described vacuum insulation trinity interchanger 3 with pipeline by variable valve.
In order to realize system DCS control, variable valve 22 installed by gaseous phase outlet pipeline 21 at BOG surge tank 2, the gas phase portion of LNG tank car 10 is connected by the pipeline 21 of pipeline 101 with described BOG surge tank 2 top, the BOG gas phase mouth of LNG tank car 10 also compresses and liquefies recovery system (or claiming pressure recovery sled) by variable valve 22 connection, the gas phase pipeline 11 on described LNG storage tank 1 top and the gas phase pipeline 81 on gas-liquid separator 8 top are respectively arranged with variable valve 12, 82, described variable valve 12, 22, 82 respectively with the temperature transmitter of pressure recovery system, pressure unit 13, 23 and 83 is chain. after the pressure in LNG storage tank 1, surge tank 2 reaches prescribed value or LNG tank car 10 has been unloaded, Controlling System is started pressure recovery sled by DCS automatically, is reclaimed by the BOG gas in LNG storage tank 1, surge tank 2 and LNG tank car 10. in order to prevent gas countercurrent flow, described pipeline 101 and the pipeline 21 on described BOG surge tank 2 top arrange vacuum breaker 102,24 respectively.
Referring to figs. 2 to Fig. 4, described vacuum insulation trinity interchanger 3 comprises shell 34 and interior courage 35, it is formed with vacuum vacuum shell 36 between described shell 34 and described interior courage 35, some heat transfer tubes 37 of described vacuum insulation trinity interchanger 3 are integrated is arranged at described interior courage 35 inside, forms heat transfer zone 32,31, two grades, one-level heat transfer zone and three grades of heat transfer zone 33. Pipe journey 39 between the one-level heat transfer zone 31 of described vacuum insulation trinity interchanger 3 and two grades of heat transfer zone 32, between two grades of heat transfer zone 32 and three grades of heat transfer zone 33 is connected by pipe journey connection chamber 391 respectively; Shell side 38 between the one-level heat transfer zone 31 of described vacuum insulation trinity interchanger 3 and two grades of heat transfer zone 32, between two grades of heat transfer zone 32 and three grades of heat transfer zone 33 is connected by shell side pipe connecting 381 respectively. In addition, the interior courage 35 of described vacuum insulation trinity interchanger 3 is laid with helical baffles 351, it is beneficial to the heat exchange effect strengthening vacuum insulation trinity interchanger.
Refer again to Fig. 1, adopt the method for the above system recoveries BOG, comprise the steps:
S1. by BOG collection and confinement of gases in LNG gas station pipeline to BOG surge tank 2, when BOG pressure reaches certain value in BOG surge tank 2, LNG storage tank 1 or after tank car unloaded, the low temperature in LNG storage tank 1, LNG tank car 10 and BOG surge tank 2 is reclaimed BOG by sending into one-level heat transfer zone 31 heat exchange of vacuum insulation trinity interchanger 3 after variable valve pressure regulation to suitable pressure and flow;
S2. in vacuum insulation trinity interchanger 3, the compression NG that low temperature reclaims BOG and normal temperature carries out one-level heat exchange, make low temperature recovery BOG temperature rise to about 20 DEG C and become normal temperature NG (Sweet natural gas), then the compressor 41 of normal temperature NG feeding expanding compress all-in-one 4 carries out one stage of compression supercharging;
S3. the first step compressor 41 of adiabatic expansion compression all-in-one 4 relies on the mechanical energy of adiabatic expansion machine 42 to drive, normal temperature NG is carried out one stage of compression supercharging, and with one-level air temperature type interchanger 5, BOG gas is cooled to normal temperature NG, normal temperature NG feeding two stage compressor 7 is carried out two grades of compressions and is pressurized to 10MPa, two stages of compression adopts inter-stage empty temperature condensation, make the NG gas temperature after compression at about 30 DEG C, then compression NG is delivered in vacuum insulation trinity interchanger 3 and cool;
S4. compress NG and carry out three grades of heat exchange with part LNG in low temperature recovery BOG, gas-liquid separator NG and gas-liquid separator respectively in vacuum insulation trinity interchanger, compression NG temperature is made to be down to about-110 DEG C, then NG is sent into the decompressor 42 of expanding compress all-in-one 4, NG pressure is made to be down to 400KPa, the temperature of NG is down to about-160 DEG C, and major part NG is liquefied as LNG;
S5. the gas-liquid mixture after adiabatic expansion is sent into gas-liquid separator 8, realize gas-liquid separation, gaseous state low temperature NG is by delivering to two grades of heat transfer zone 32 heat exchange of vacuum insulation trinity interchanger 3 after variable valve 82 pressure regulation, a LNG part is pumped to LNG storage tank 1, another part delivers to two grades of cooled compressed NG heat exchange of pipe journey connection chamber 391 (namely between two grades of heat transfer zone and three grades of heat transfer zone) between three grades of heat transfer zone 33 shell sides of vacuum insulation trinity interchanger 3 and two or three grades, temperature rises to-120 DEG C and gasifies, two grades of heat transfer zone 32 shell side cooled compressed NG of three grades of tubular heat exchangers 3 are entered together with the low temperature NG gas from gas-liquid separator 8 after entering two grades of heat transfer zone 32 by shell side pipe connecting 381 between two or three grades after LNG gasification, go out the shell side pipe connecting 381 of two grades of heat transfer zone 32 between one or two grades (namely between one-level heat transfer zone with two grades of heat transfer zone) to enter one-level heat transfer zone 31 shell side 38 and reclaim with low temperature, together with BOG, the compression NG gas entering one-level heat transfer zone 31 pipe journey 39 is carried out first step heat exchange.
The mechanical energy produced when the present invention adopts low temperature BOG adiabatic expansion to freeze drives compressor, the BOG after rich heat is carried out one stage of compression simultaneously, reduces energy consumption, it is to increase refrigerating efficiency; Adopt vacuum insulation three-in-one spiral traverse baffle shell and tube heat exchanger to realize the liquefy cold energy of each workshop section of BOG compression refrigeration to make full use of, enhance heat transfer efficiency, it is to increase the liquefaction efficiency that BOG reclaims; DCS is adopted to be controlled by BOG pressure recovery sled, safe and reliable, simple to operate, it is beneficial to the potential safety hazard reducing LNG gas station, it is possible to realize BOG gas high efficiente callback, thus avoids BOG gas emptying to process the environmental pollution and the wasting of resources caused.
The foregoing is only the schematic embodiment of the present invention, it does not mean to limit the scope of the present invention. As vacuum insulation three-in-one spiral traverse baffle shell and tube heat exchanger can also adopt more than three grades or the realization of other form multi-stage heat exchanger structures; the technician of any this area; equivalent variations done under the prerequisite of the design and principle that do not depart from the present invention and amendment, all should belong to the scope of protection of the invention.
Claims (8)
1.LNG gas station BOG compresses and liquefies recovery system, comprises the LNG storage tank for storing LNG liquid (1) and the BOG surge tank (2) for collecting BOG gas in gas station pipeline; It is characterized in that: LNG storage tank (1) is connected with the one-level heat transfer zone (31) of vacuum insulation trinity interchanger (3) by pipeline (11,21) respectively with described BOG surge tank (2); The compressor (41) that all-in-one (4) is compressed with adiabatic expansion in the one-level heat transfer zone (31) of described vacuum insulation trinity interchanger (3) is connected, the compressor (41) of described adiabatic expansion compression all-in-one (4) is connected with two stage compressor (7) by one-level air temperature type interchanger (5), and described two stage compressor (7) is connected with the one-level heat transfer zone (31) of vacuum insulation trinity interchanger (3) by two grades of air temperature type interchanger (6); The adiabatic expansion machine (42) that three grades of heat transfer zone (33) of described vacuum insulation trinity interchanger (3) compress all-in-one (4) with adiabatic expansion is connected; The adiabatic expansion machine (42) of described adiabatic expansion compression all-in-one (4) connects gas-liquid separator (8), the gas phase mouth of described gas-liquid separator (8) is connected with two grades of heat transfer zone (32) of described vacuum insulation trinity interchanger (3) with variable valve (82) by pipeline (81), the liquid phase mouth of described gas-liquid separator (8) connects cryopump (9), and described cryopump (9) is connected with three grades of heat transfer zone (33) and the described LNG storage tank (1) of described vacuum insulation trinity interchanger (3).
2. LNG gas station BOG as claimed in claim 1 compresses and liquefies recovery system, it is characterised in that: three tubular heat exchangers are integrated in a vacuum shell by described vacuum insulation trinity interchanger (3), are provided with helical baffles in vacuum shell.
3. LNG gas station BOG as claimed in claim 1 compresses and liquefies recovery system, it is characterized in that: described adiabatic expansion compression all-in-one (4) drives compressor (41) while adopting adiabatic expansion machine (42) to carry out freezing, the BOG after rich heat is carried out one stage of compression.
4. LNG gas station BOG as claimed in claim 1 compresses and liquefies recovery system, it is characterized in that: be respectively arranged with variable valve (12,22,82) on pipeline (11,21,81), described variable valve (12,22,82) is mutually chain with pressure unit, temperature transmitter and fluid level transmitter respectively.
5. LNG gas station BOG as claimed in claim 1 compresses and liquefies recovery system, it is characterized in that: the gas phase portion of LNG tank car (10) is connected with the pipeline (21) on described BOG surge tank (2) top by pipeline (101), and pipeline (101,21) arranges vacuum breaker (102,24) respectively.
6. LNG gas station BOG as claimed in claim 1 compresses and liquefies recovery system, it is characterized in that: described vacuum insulation trinity interchanger (3) comprises shell (34) and interior courage (35), vacuum shell (36) is formed between described shell (34) and interior courage (35), some heat transfer tubes (37) of described vacuum insulation trinity interchanger (3) are integrated to be arranged at described interior courage (35) inside and forms described one-level heat transfer zone (31), two grades of heat transfer zone (32) and three grades of heat transfer zone (33), each heat transfer zone tubular heat exchanger adopts helical baffles to improve heat transfer efficiency.
7. LNG gas station BOG as claimed in claim 6 compresses and liquefies recovery system, it is characterised in that: the Guan Cheng (39) between the one-level heat transfer zone (31) of described vacuum insulation trinity interchanger (3) with two grades of heat transfer zone (32), between two grades of heat transfer zone (32) and three grades of heat transfer zone (33) passes through pipe journey connection chamber (391) respectively and is connected; Shell side (38) between the one-level heat transfer zone (31) of described vacuum insulation trinity interchanger (3) with two grades of heat transfer zone (32), between two grades of heat transfer zone (32) and three grades of heat transfer zone (33) is connected by shell side pipe connecting (381) respectively.
8. adopt the method for system recoveries BOG as claimed in claim 7, it is characterised in that, comprise the steps:
S1. being collected in BOG surge tank by the pipeline BOG of LNG gas station, and install variable valve at the gaseous phase outlet of BOG surge tank, the gas phase of LNG tank car also connects pressure recovery sled by this variable valve; The gaseous phase outlet of LNG storage tank is installed variable valve and is connected with pressure recovery sled; The pressure treated in storage tank exceedes the requirement of regulation, and chain promoter pressure recovery is prized by DCS, is reclaimed by BOG gas in LNG storage tank, and after LNG storage tank pressure is reduced to the value of regulation, DCS will stop pressure recovery; When BOG surge tank pressure reaches certain value, chain promoter pressure recovery is prized by DCS, and after pressure is reduced to the pressure of regulation, pressure recovery device will stop automatically; After LNG tank car has been unloaded, by pressure recovery sled, NG in tank car is fully reclaimed; The vacuum insulation trinity interchanger that the BOG gas reclaimed sends into recovery device of liquefied respectively after pressure regulation carries out one-level heat exchange, fully reclaims the cold energy of BOG gas;
S2. in vacuum insulation trinity interchanger, the compression NG of low temperature BOG gas and normal temperature carries out one-level heat exchange, makes BOG gas temperature rise to 15��25 DEG C, becomes NG, by its cold energy all by compressing rear NG gas recovery;
S3. then NG is sent into first step compressor boost, stage compressor utilizes the mechanical energy of adiabatic expansion refrigerator to drive, NG after compression sends into high stage compressor, it is compressed to 10MPa, two stages of compression adopts inter-stage condensation, make the NG gas temperature after compression control at 25��35 DEG C, then compression NG is delivered to vacuum insulation trinity interchanger and lowers the temperature;
S4. compress NG in vacuum insulation trinity interchanger, to reclaim after BOG, gas-liquid separator part LNG in NG and gas-liquid separator respectively with low temperature carry out three grades of heat exchange, make compression NG gas temperature be down to-105��-115 DEG C; Then NG sending into adiabatic expansion machine, makes NG pressure be down to 400KPa, owing to NG thermal insulation acting temperature is down to-155 DEG C��-165 DEG C, major part NG is liquefied;
S5. gas-liquid mixture is sent into gas-liquid separator, it is achieved gas-liquid separation; Gaseous state low temperature NG is by delivering to the two grades of heat exchange of vacuum insulation trinity interchanger after variable valve pressure regulation, a LNG part is pumped to LNG storage tank, and another part delivers to the vacuum insulation trinity interchanger third stage and compression NG heat exchange; In three grades of heat transfer zone, LNG temperature rises to-120 DEG C and is gasificated into low temperature NG, the low temperature NG going out three grades of heat transfer zone enters the two grades of heat exchange of vacuum insulation trinity interchanger by shell side pipe connecting in vacuum insulation trinity interchanger together with gas-liquid separator low temperature NG, and heat exchange enters one-level heat transfer zone and cooled by compression NG gas together with reclaiming BOG after terminating; Enter two grades of heat transfer zone from inter-stage pipe journey chamber respectively after compression NG is cooled from one-level heat transfer zone, after two grades of coolings, enter again three grades of heat transfer zone enter cooling.
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